DE69917280T2 - METHOD FOR THE PRODUCTION OF POLYMERS BY A FREE RADICAL PROCESS, POLYMERIZATION AND CONDENSATION REACTION AND APPARATUS THEREFOR, AND MANUFACTURED PRODUCTS - Google Patents

Abstract

The present invention provides a high temperature continuous polymerization and condensation process for preparing a polymeric product. The process includes continuously charging into a reaction zone: at least one radically-polymerizable monomer having a radically polymerizable group and at least one condensation reactive functionality; and at least one modifying agent having a functional group capable of reacting with the condensation reactive functionality. The reaction zone includes at least one primary reactor, but may, and preferably does, contain a secondary reactor. The process further includes maintaining an effective temperature in the primary reactor to cause polymerization of the monomer and to allow at least a portion of the condensation reactive functionality to react with the functional group of the modifying agent.

Description

REFERENCE TO A RELATED REGISTRATION

These Application claims the benefit of provisional patent application no. 60/092433, filed July 10, 1998, at the time of its publication is hereby incorporated by reference.

FIELD OF THE INVENTION

The The present invention generally relates to a continuous one Polymerization and condensation process for the conversion of a radically polymerizable monomer with a condensation reactive functionality and a modifier having a functional group, which is capable of reacting with the condensation-reactive functionality to a polymer product. The invention also relates to polymer products, which are produced by the process, and various products, containing the polymer product.

BACKGROUND THE INVENTION

method for the preparation of polymers are well known in the art known. Many methods that are used today for polymers for the industrial application, but suffer from considerable Restrictions, including high cost, significant gelation problems, if a high degree in functionality exists and the inability to Polymers with special desired To produce properties.

The U.S. Patent No. 4,414,370 describes a continuous bulk polymerization process for the polymerization of vinyl monomers to lower polymers Produce molecular weight, which is a thermal start at reaction temperatures from 235 ° C up to 310 ° C and residence times of at least 2 minutes in a continuous stirred Reactor zone comprises. The vinyl monomers of the published method include Styrenic monomers such as styrene and α-methylstyrene; acrylic monomers, such as acrylic acid, methacrylic acid, Acrylates and methacrylates; and other non-acrylic ethylene monomers, such as vinyl acetate.

The U.S. Patent No. 4,529,787 describes a continuous bulk polymerization process, which comprises a starter for the preparation of uniform polymers low molecular weight vinyl monomer with short residence times and moderate reaction temperatures, gives the high yield of a product which is suitable for high strength Applications is suitable. The vinyl monomers described include Styrenic monomers such as styrene and α-methylstyrene; acrylic monomers, such as acrylic acid, methacrylic acid, Acrylates, methacrylates and acrylic functional monomers; and non-acrylic Ethylene monomers such as maleic anhydride and vinylpyrrolidinone.

The U.S. Patent No. 4,546,160 describes a continuous bulk polymerization process for the polymerization of acrylic monomers for the production of uniform Low molecular weight polymers for use in high strength applications, which has a low amount of starter with short residence times and moderate temperatures used.

It Various attempts have been made to the physical To improve properties of polymers by adding a type of polymerizable Monomer was replaced by another, or by reaction of a Polymers with a group incorporated into the polymer structure becomes. For example, U.S. Patent No. 5,130,369 teaches Process for the preparation of functionalized polymer compositions.

The U.S. Patent No. 5,521,267 describes a method of manufacture of polymers of ethylenically unsaturated compounds, the acid groups containing, with other ethylenically unsaturated compounds and monohydroxy compounds.

It there is no publication about that, as a polymerization and condensation process in continuous High conversion mode can be done so that gelation in such procedures can be avoided, where due to the multiple functionality one or more components networking is possible.

In The polymer industry has long been known to use continuous polymerization processes useful are big Obtain quantities of a polymer product. In addition, provide continuous Process economic Advantages over Bulk polymerization and may be more uniform polymer products to disposal put. Furthermore are many radically polymerizable monomers that are desirable containing modifying groups, significantly more expensive than the precursors, from which they are made. During continuous process for the preparation of certain polymer products for use in high strength Coating applications published Thus, there is a need for a continuous high temperature process for the preparation of polymer products with improved properties, by reaction conditions and introducing a desired Modifier can be achieved in the reaction zone. Continue to exist a need for a continuous polymerization process a modifier with a high degree of conversion in a polymer chain is incorporated while at the same time it is possible to influence the structure of the polymer chain.

SUMMARY OF THE INVENTION

It would be extraordinary desirable, a polymer product using a continuous polymerization and to be able to produce a condensation reaction in which a modifier is incorporated into the polymer chain in the reaction zone during gelation is avoided and possible is to influence the structure of the polymer chain.

• (a) kontinuierliches Einbringen in einen Polymerreaktor:
• (i) mindestens ein radikalisch polymerisierbares Monomer mit einer radikalisch polymerisierbaren Gruppe, das auch mindestens eine kondensationsreaktive Funktionalität aufweist; und
• (ii) mindestens ein Modifizierungsmittel mit einer funktionellen Gruppe, die in der Lage ist, mit der kondensationsreaktiven Funktionalität am radikalisch polymerisierbaren Monomer zu reagieren, wobei jedes Modifizierungsmittel ein Monohydroxyalkohol ist, und wobei jedes Modifizierungsmittel nicht die Formel ROH hat, in der R ein lineares oder verzweigtes Alkylradikal mit mehr als 11 Kohlenstoffatomen ist; und
• (b) Aufrechterhalten einer effektiven Temperatur im Primärreaktor, um die Polymerisation des Monomers hervorzurufen und mindestens einem Teil der kondensationsreaktiven Funktionalität zu ermöglichen, mit der funktionellen Gruppe des Modifizierungsmittels zu reagieren, wobei ein erstes Polymerprodukt hergestellt wird, das mindestens einen Teil des Modifizierungsmittels enthält, und wobei das gebildete Polymerprodukt praktisch frei von Gelbildung ist.

An object of the present invention is to provide a continuous polymerization and condensation process comprising:

• (a) continuous introduction into a polymer reactor:
• (I) at least one radically polymerizable monomer having a radically polymerizable group which also has at least one condensation-reactive functionality; and
• (ii) at least one modifier having a functional group capable of reacting with the condensation-reactive functionality on the radically-polymerizable monomer, wherein each modifier is a monohydric alcohol, and wherein each modifier does not have the formula ROH in which R is a linear or branched alkyl radical having more than 11 carbon atoms; and
• (b) maintaining an effective temperature in the primary reactor to cause the polymerization of the monomer and to allow at least a portion of the condensation reactive functionality to react with the functional group of the modifier to produce a first polymer product containing at least a portion of the modifier; and wherein the polymer product formed is virtually free of gelation.

The Invention further provides an imprint varnish, a coating, a coating modifier and a coating compatibility agent, a dispersant, a polymeric surfactant or a paint to disposal, containing a polymer product that after the continuous Polymerization and Condensation process according to the invention was obtained. In some preferred methods, at least two different radically polymerizable monomers in one primary reactor introduced while in other preferred embodiments the radically polymerizable monomer at least two condensation-reactive functionalities having. In some preferred processes, the modifier has a functional group that is capable of reacting with the condensation functionality to react while other preferred methods modifier with more than one such functional group. In some preferred methods are the two functional groups on the multifunctional modifier same, while they are different from each other in other processes. Multifunctional Modifiers can polymeric or non-polymeric, and in various preferred Process is both a monofunctional modifier, as well as a multifunctional, non-polymeric modifier used.

One Polymer product of the process may contain a cyclohexyl group, and in preferred processes that is free radically polymerizable Monomer acrylic acid and the modifier cyclohexanol. In other preferred Process, at least one vinyl aromatic monomer is continuous in the primary reactor introduced while in other preferred methods at least two different vinyl aromatic Monomers are introduced into the reaction zone.

In preferred method, the condensation-reactive functionality is a carboxyl, an ester, anhydride, a hydroxy, an epoxy, an amine, a ketone, an aldehyde or an isocyanate functionality, while in other preferred methods the functional group of the modifier a carboxyl, a hydroxy, an anhydride, an amine, a Epoxy or isocyanate group.

In various preferred methods, the temperature in the primary reactor between 175 ° C and 345 ° C kept while in other preferred methods, the temperature is maintained above 300 ° C. In yet other preferred methods, the flow rate through the primary reactor adjusted so that they have a mean residence time of 60 minutes or less in the primary reactor to disposal provides.

In some preferred methods will be one or more additional ones Components, such as a radically polymerizable Monomer, which is virtually free of condensation reactive groups, a inert solvent, a means for separating by-products or a starter too one or more reactors added in the process while in Another preferred method is a catalyst such as an esterification, transesterification or amidation catalyst, is added to one of the reactors. In still other preferred Procedure, the reaction zone is virtually free of an inert Solvent.

In Still other preferred methods further include the method a secondary reactor, and the method further comprises introducing the first polymer product from the primary reactor in the secondary reactor and subsequent Removing a second polymer product from the secondary reactor. In In some preferred processes, the primary reactor is continuous stirred stirred tank reactor or a cycle reactor while in other preferred embodiments the secondary reactor a circulation reactor, a tubular reactor, an extruder reactor or a stirred stirred tank reactor, or any one Reactor for suitable for continuous operation. In still other preferred Process, at least one of the polymer products is continuous placed in an extruder reactor, and additional modifier is introduced into the extruder reactor to produce a polymer product. The product may be further modified into a discontinuous one Reactor be given. In still other preferred method differ the temperatures in the primary and secondary reactor from each other, and preferably they are controlled independently.

In various preferred methods will be at least part of the Modifier introduced into the secondary reactor while in other preferred methods, the modifier in two different Reaction zones in the secondary reactor is introduced. In still other preferred methods, at least two different modifiers in each one of two introduced different reaction zones in the secondary reactor.

In preferred method comprises at least one reactor in the reaction zone a headspace, and the method includes flushing the headspace with a headspace Inert gas. In more preferred methods, a volatile Material from the primary reactor separated to two streams to create. One of the streams is relatively free of byproducts while the other stream is unreacted Contains starting materials. In preferred methods, the stream is relatively free of byproduct is fed to a reactor in the reaction zone.

BRIEF DESCRIPTION OF THE DRAWINGS

The preferred exemplary embodiment The invention will be described below in conjunction with the appended drawings wherein like numbers represent like elements, and:

1 Figure 3 is a schematic diagram of a polymerization reactor network used in the present invention; and

2 Fig. 12 is a schematic diagram of a polymerization reactor network used in the present invention, in which a conventional evaporator is interposed between the primary and secondary reactors.

DETAILED DESCRIPTION OF THE INVENTION

The The present invention provides continuous processes for the production of polymer compositions by free radical polymerization in the presence of one or more modifiers. Of the Term "continuous" is defined here as a method in which a reactant, such as a Modifying agent and / or a radically polymerizable Monomer is introduced into a reactor while a polymer product simultaneously while is separated at least part of the reaction process.

The Invention allows the incorporation of modifiers up to a relatively high Degree, as he used to not in conventional free radical polymerization possible was what made it possible To obtain high molecular weight polymer products at high temperatures, get crosslinked polymer products, and a method of modification the molecular structure of polymer products available to deliver.

in the generally includes a continuous polymerization and condensation process according to the present Invention the continuous introduction of at least one radical polymerizable monomer and at least one modifier in a reaction zone. The reaction zone has at least one primary reactor, but preferably also includes a secondary reactor. The radically polymerizable Monomer has a radically polymerizable group and has moreover at least one condensation-reactive functionality. The modifier has at least one functional group that is able to interact with the condensation-reactive functionality on the free-radically polymerizable Reacting monomer, wherein each modifier is not the ROH has a linear or branched alkyl radical with is more than 11 carbon atoms. The temperature in the primary reactor is kept at an effective temperature, which is the polymerization of the monomer and makes it possible that at least a part of the condensation-reactive functionality with the functional group of the modifier reacts. In this way a polymer product is obtained which contains at least a part of the Including modifier, and the polymer product is formed with virtually no gelation.

The Reaction between the condensation-reactive functionality of the radical polymerizable monomer and the functional group of the modifier is a condensation reaction, not a free radical polymerization mechanism. Condensation reactions are well known in the art, and are defined here as any reaction that the combination of two molecules comprises to form a larger molecule, being a molecule has at least one functional group that is able to with a condensation-reactive functional group at the other molecule to react. The condensation reaction can with the elimination a small molecule go along or not. The small molecule that undergoes a condensation reaction is eliminated as a condensation by-product or by-product designated. examples for some preferred condensation reactions include esterification reactions, Transesterification reactions and amidation reactions. Although transesterification reactions not always to the formation of a large molecule as a product and a small one molecule as by-product, they are usually classified as condensation reactions and hereinafter also referred to as such. Condensation reactions can be self-catalyzed be, or you can alternatively by a large one Variety of catalysts are catalyzed as condensation catalysts be designated. As mentioned, the modifier becomes the final polymer product of the process of the invention built-in. The incorporation of the modifier gives the polymer product desirable Properties and needed in the general less expensive precursors and other materials as an alternative Procedure to achieve this result.

The Free-radically polymerizable monomer used in the process contains a or more condensation reactive functionalities. Examples of suitable condensation-reactive functionalities of the radically polymerizable Monomers include carboxy, hydroxy, anhydride, amine, epoxy, Isocyanate, ketone, aldehyde, amide and ester functionalities.

Various carboxyl and ester containing radically polymerizable monomers can be used in the continuous high temperature polymerization and condensation process. Examples of carboxyl-containing radically polymerizable monomers include acrylic acid, methacrylic acid and maleic acid. Examples of ester-containing, radically polymerizable monomers include acrylates, methacrylates, diacrylates and dimethacrylate monomers. Preferred examples include, but are not limited to, butyl acrylate, 2-ethylhexyl acrylate, cyclohexyl acrylate, cyclohexyl methacrylate, ethyl acrylate, methyl acrylate, methyl methacrylate, isobutyl acrylate, isobutyl methacrylate, butyl methacrylate, ethylene glycol diacrylate, ethylene glycol dimethacrylate and 1,6-hexanediol diacrylate. Other examples of ester-containing, radically polymerizable monomers include 1-butylaminoethyl methacrylate, 2-chloroethyl methacrylate, 2-ethoxyethyl methacrylate, 2-ethylbutyl methacrylate, 2-ethylhexyl methacrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl methacrylate, 2-methoxybutyl methacrylate, 2-n-butoxyethyl methacrylate, 2-nitro -2-methylpropyl methacrylate, 2-phenoxyethyl methacrylate, 2-phenylethyl methacrylate, 2-sulfoethyl methacrylate, 3-methoxybutyl methacrylate, allyl methacrylate, benzyl methacrylate, butylaminoethyl methacrylate, Cinnamylmethacrylat, crotyl methacrylate, cyclopentyl methacrylate, ethyl acrylate, ethyl methacrylate, furfuryl methacrylate, glycidyl methacrylate, hexafluoroisopropyl methacrylate, isoamyl methacrylate, isobutyl methacrylate, isopropyl acrylate, isopropyl methacrylate , Methyl 2-cyanoacrylate, methyl acrylate, methyl α-chloroacrylate, n-amyl methacrylate, n-butyl methacrylate, n-decyl acrylate, n-hexyl methacrylate, N, N-diethylaminoethyl methacrylate, N, N-dimethylaminoethyl methacrylate, n-octyl methacrylate at, n-propyl acrylate, n-propyl methacrylate, phenyl methacrylate, sec-butyl methacrylate, t-butyl methacrylate, tetrahydrofurfuryl methacrylate, tetrahydropyryl methacrylate and trifluoroethyl methacrylate.

The Radically polymerizable monomer can also be an anhydride, a ketone, an aldehyde, an epoxy or a hydroxy condensation reaction functionality contain. examples for anhydride-containing, radically polymerizable monomers include maleic anhydride, itaconic and citraconic anhydride. examples for ketone- and aldehyde-containing, radically polymerizable monomers include methacrolein, methyl vinyl ketone and acrolein. Examples for epoxy-containing, radically polymerizable monomers for use in the process include glycidyl methacrylate, glycidyl acrylate and 4-vinyl-1-cyclohexene-1,2-epoxide. Hydroxy-containing, radically polymerizable monomers which are used in the process can be used include hydroxy acrylates and methacrylates such as 2-hydroxyethyl methacrylate, 2-hydroxyethyl acrylate, hydroxypropyl acrylate, 3-chloro-2-hydroxypropyl acrylate, 2-hydroxybutyl acrylate, 6-hydroxyhexyl acrylate, 2-hydroxymethyl methacrylate, 2-hydroxypropyl methacrylate, 6-hydroxyhexyl methacrylate and 5,6-dihydroxyhexyl methacrylate.

Various amine and isocyanate-containing monomers can be used in the continuous high-temperature polymerization and condensation methods are used. Examples of amine-containing, radically polymerizable monomers include 2- (diethylamino) ethyl acrylate, 2- (dimethylamino) ethyl acrylate, 2- (dimethylamino) propyl acrylate, 2- (diethylamino) ethyl methacrylate, 2- (dimethylamino) ethyl methacrylate and 2- (dimethylamino) propyl acrylate. examples for isocyanate-containing monomers include 3-isopropenyl-α, α-dimethylbenzyl isocyanate and 2-isocyanatoethyl methacrylate.

Yet other radically polymerizable monomers that are condensation reactive functionalities include amides such as acrylamide, N-ethylacrylamide, N, N-diethylacrylamide, methacrylonitrile, methacrylamide, N-methylmethacrylamide, N-ethylmethacrylamide, N, N-diethylmethacrylamide, N, N-dimethylmethacrylamide and N-phenylmethacrylamide.

The functional group of the modifier that is able to with the condensation-reactive functionality on the free-radically polymerizable Monomer includes carboxyl, hydroxy, anhydride, amine, Epoxy, ketone, aldehyde, ester and isocyanate groups. The modifier comprises one or more such functional groups, and at least some of the functional groups react with the condensation reactive functionalities on radically polymerizable monomer. In addition, a can or several different modifiers in the different ones Method of the invention can be used.

In contains preferred method the modifier only one functional group. Such modifiers called monofunctional modifiers.

Examples for hydroxy containing, monofunctional modifiers include aliphatic, alicyclic, aromatic and aromatic alkyl alcohols and derivatives thereof. Other Examples include halo alcohols, such as fluoroalkyl alcohol, Dodecafluoroheptanol, octafluoropentanol and heptafluoroisopropanol. Further examples for Alcohols include hindered amine light stabilizers, such as For example, N-methyl-2,2,6,6-tetramethyl-4-piperidinol and 2,2,6,6-tetramethyl-4-piperidinol. Preferred modifiers, the hydroxyl-containing, condensation-reactive Contain groups include primary and secondary Alcohols. Exemplary primary Alcohols include cyclohexylmethanol, 4-methylcyclohexylmethanol and cyclohexylethanol, propanol, butanol, 2-ethylhexanol and diethylene glycol monoethyl ether, while exemplary secondary Alcohols cyclohexanol, isopropanol, isobutanol, isooctanol and isoborneol include. In a preferred embodiment, the modifier is not an alcohol of the formula ROH, wherein R is a straight chain or branched alkyl group having 12 or more carbon atoms.

In a preferred method the modifier is a carboxyl functional group. For example For example, preferred monofunctional modifiers include cyclohexanecarboxylic acid.

Other preferred monofunctional modifiers include an amine functional Group. The amine functional group can be a primary amine or a secondary one Be amine. examples for primary and secondary amine-containing, monofunctional modifiers include ethylamine, Propylamine, butylamine, cyclohexylamine, isopropylamine, benzylamine and polyetheramines.

In other preferred methods, the modifier contains more than one functional group capable of having the condensation reactive functionality on the radically polymerizable monomer to react. These modifiers are referred to as multifunctional modifiers. The multifunctional modifier may have more than one functional group capable of reacting with the monomer or, alternatively, the multifunctional modifier may have only one functional group capable of reacting with the condensation reactive groups, and the other remaining functional groups are capable of reacting with each other to generate crosslinks in the polymer. In a preferred process, hydroxyethyl methacrylate is used as the radically polymerizable monomer and adipic acid as the multifunctional, non-polymeric modifier.

In a more preferred method has a multifunctional, non-polymeric modifier more than one functional group that is capable of having one condensation-reactive functionality on radically polymerizable To react monomer with a condensation-reactive functionality. In this way, cross-linking and branching in the polymer product introduced by that the multifunctional modifier in at least two various polymer chains is incorporated. In this preferred Process comprises the multifunctional, non-polymeric modifier difunctional, trifunctional and other species with a higher degree of functionality. The use of a non-polymeric, functional modifier in the polymerization and Condensation reaction leads to an increase in the molecular weight of the polymer product. If, for example Ethylene glycol as a modifier together with acrylic acid as free radically polymerizable monomer has the polymer product the polymerization and condensation reaction increased molecular weight. As the molecular weight of polymers by free radical polymerization normally decreases when the process temperature increases, especially if chain termination by cleavage occurs, provides a method using a multifunctional Modifier a method for increasing the molecular weight of the polymer product at high polymerization temperature. Because the molecular weight of most non-polymeric, multifunctional modifier is small, one needs only small amounts by weight to substantial increases in the molecular weight of the polymer products to reach.

preferred multifunctional, non-polymeric modifiers those containing a hydroxy functionality. Examples of such hydroxy-containing multifunctional, non-polymeric modifier include ethylene glycol, tri (ethylene) glycol, butylene glycol, propylene glycol, Di (propylene) glycol, Neopentyl glycol, glycerol, cyclohexanedimethanol, 2-methyl-1,3-propanediol, 3-methyl-2,4-pentanediol, 1,10-decanediol, 1,6-hexanediol, 1,5-pentanediol, Pentaerythritol, trimethylolethane and trimethylolpropane. Like here used, the term "monohydric alcohol" defines any alcohol that is only a single OH functionality has. Monohydroxy alcohols include, but are not limited to aromatic, cyclic and aliphatic alcohols, both saturated and also unsaturated. In one embodiment the modifier is not a monohydric alcohol, and some or all reactors are free of monohydric alcohols. In a another embodiment For example, the modifier includes diols, triols, tetraols and others multifunctional alcohols, but is not limited thereto. In another preferred embodiment contain one or more reactors only monohydroxy alcohols as Modifier, wherein the monohydroxy alcohols are not of the formula ROH, wherein R is a linear or branched alkyl moiety is more than 11 carbon atoms. In yet another preferred embodiment When several modifiers are used in a single reactor, wherein at least one of the modifiers used in the individual reactor is not a monohydric alcohol.

Other preferred multifunctional modifiers include cyclic ones Esters and amides. These include, but are not limited to Structures such as Formula 1 wherein n is 0-7 and X is = S, O or N can be. These materials can be used if the functional monomer is an acid or hydroxyl having. The resulting polymer product receives side chains from the polymer sequences. Such polymers are described as comb-like and can be used in this process without the risk of substantial gelation getting produced. Professionals in the field will recognize that one Combination of different non-polymeric, multifunctional Modifying agents, each being at least two different Types of functional groups included in this method in different proportions can be used to make a polymer product with desired To get properties.

FIG. 1

Other preferred multifunctional, non-polymeric modifiers include the amine functionality. examples for amine-containing multifunctional, non-polymeric modifiers include hexamethylenediamine, p-phenylenediamine, ethylenediamine, isofurondiamine and 2-methyl-1,5-pentanediamine.

Yet other preferred multifunctional, non-polymeric modifiers include those having carboxyl or anhydride functionality. Examples for this multifunctional, non-polymeric modifier adipic acid, azelaic acid, trimesic phthalic acid, isophthalic acid, dodecanedioic, terephthalic acid, 1,4-cyclohexanedicarboxylic acid, sebacic acid and Trimellitic.

Other preferred multifunctional, non-polymeric modifiers include a combination of functional groups that exist in the Capable of reacting with condensation reactive functionalities. The condensation-reactive functionalities with which the functional Groups of these multifunctional, non-polymeric modifiers preferably include carboxyl, hydroxy, amine, ester, anhydride, isocyanate and epoxy reactive Functionalities. Thus, certain preferred multifunctional, non-polymeric Modifier at least two different types of functional Groups that are able to react with condensation-reactive functionalities on a radical basis polymerizable monomers to react. The different types of functional groups on these multifunctional modifiers are preferably able to react with each other to sequences of combined modifier units which form can be incorporated into the polymer.

In In other preferred methods, the modifier is one amino acid or a hydroxy acid. examples for preferred amino acid modifier include alanine, glycine, lysine, leucine, isoleucine and phenylalanine, while examples for Hydroxy acid modifiers glycolic acid, Lactic acid, mandelic acid, benzylic acid, 4-hydroxybutanoic acid, 12-hydroxystearic acid and 12-hydroxydodecanoic acid.

Other preferred multifunctional non-polymeric modifiers have only two functional groups which are different and capable of reacting with condensation reactive functionalities on radically polymerizable monomers. Still other preferred multifunctional non-polymeric modifiers have the structure HO-RC (= O) OH or H ₂ NRC (= O) OH, where R is a linking chemical group such as a chain of methylene units, an aromatic group or a combination designated by these. This class of multifunctional non-polymeric modifiers can react with other such modifiers to form linear polymer sequences represented by the formula HO- (RC (= O) O) _n -RC (O =) OH or H ₂ N - (RC (= O) N (H)) _n -RC (= O) OH, where n is a variable greater than or equal to 1. In more preferred methods, the radically polymerizable monomer contains carboxyl or hydroxy functionalities, and the modifier is multifunctional, non-polymeric and has the structure HO-RC (O =) OH or H ₂ NRC (= O) OH as described above. The resulting polymer product contains side chains from the polymer sequences. Such polymers are described as comb-like and can be made in this process without the risk of substantial gelation. Those skilled in the art will recognize that a combination of various non-polymeric multifunctional modifiers, each containing at least two different types of functional groups, can be used in various proportions in this process to obtain a polymer product having the desired properties.

A functional group of multifunctional non-polymeric modifiers bearing more than one functional group can more or less readily react as the other with the condensation reactive functionality on a radically polymerizable monomer. In this way, dual functional polymer products can be made by the polymerization and condensation reaction process. In preferred methods, the less reactive functional group can be attached to such a mul tifunctional modifier be sterically hindered.

In Polymerization and condensation processes of the invention may include Reaction conditions selected be that while the polymerization only a partial conversion of the multifunctional, non-polymeric Modifier takes place. This forms another method to provide a dual functionality polymer product.

More As a type of modifier can be used in the polymerization and Condensation method can be used. For example, include preferred methods are both a multifunctional, non-polymeric and a monofunctional modifier. This combination of modifiers it that high levels of monofunctional modifier incorporated into the polymer without the molecular weight of the polymer product to sacrifice. In general leads an increase the temperature in the primary Polymerization reactor and optionally in the secondary polymerization reactor to a high conversion of the monofunctional modifier. As previously noted, lead however increased Temperatures in the reaction zone in general to polymer products with reduced molecular weight. The addition of the multifunctional, non-polymeric Modifier allows a sufficient cross-linking to a polymer product with sufficient Molecular weight and a high degree of incorporation of the monofunctional modifier to disposal to deliver. In preferred methods of this kind, this includes radically polymerizable monomer has a carboxyl functionality that is monofunctional Modifier, a hydroxy-functional group, and the multifunctional, Non-polymeric modifier is a difunctional, hydroxy containing Modifiers, such as but not limited to Ethylene glycol or cyclohexanedimethanol.

preferred Modifiers also include both monofunctional and multifunctional polymeric modifiers. Such polymers Modifiers include both linear and branched ones polymeric modifiers. Examples of polymeric modifiers include polyesters, polyamides, polyethers, polyurethanes, polyacrylates and polyorganosiloxanes, in addition to other polymers containing functional groups which are able to radically with the condensation-reactive functionality polymerizable monomer to react. Examples of polyether modifiers include polyethylene glycol, polybutylene glycol, polypropylene glycol and derivatives and combinations thereof. A built-in polymer Modifier can account for a significant portion of the final mass make up a polymer product. For example, the polymeric Modifier 5 to 90 percent by weight of the final polymer product turn off. The incorporation of a polymeric modifier can also the final one Give polymer product important properties, such as Flexibility, adhesion and toughness. Polymer products made from polymeric modifiers were, can a residual functionality have, and can thus be further reacted in a Nachpolymerisationsreaktion.

in the In general, the polymer product from the polymerization and Condensation process a mixture of different proportions of radically polymerized polymer having side chains of polymeric Modifiers extending from the chains (i.e. only one reactive group of the modifier has reacted), a crosslinked polymer, wherein a multifunctional, polymeric Modifier crosslinks between different chains of the radically polymerized polymer, unreacted modifier and chains of radically polymerized polymer that are not polymeric Contain modifiers include. While it is not necessary that a substantial conversion of the modifier by Installation in the polymer is achieved, such is extensive Conversion possible using the methods of the invention. alternative Processes of the invention provide a polymer product where only some of the condensation reactive groups on the polymeric modifier react.

The radically polymerizable monomer becomes a primary reactor supplied and optionally, a portion of the monomer may be in subsequent reactors are introduced when a series of reactors is used. The modifier can either be in a primary reactor or, in a process using two reactors, in the secondary reactor or in any subsequent reactor. alternative The modifier can be used in both the primary reactor and the secondary reactors as well as any other reactors are introduced. Either The monomer as well as the modifier can be prepared by methods that are well known in the art, are added to the reactor, including Dissolve the modifier in the feed mixture or separate introduction of the Modifier in the reactor as a solid or liquid according to a method known from the prior art, including, but not limited on melting, pumping and extruding.

The Reaction between the functional group on the modifier and the condensation-reactive functionality on the free-radically polymerizable Monomer can be made in at least two ways. First, that Modifier with the radically polymerizable monomer react before it is polymerized, creating a new radical polymerizable monomer is formed, in which the modifier already installed. Alternatively, the modifier with the condensation-reactive functionality of the free-radically polymerizable Monomers react after the radically polymerizable monomer was incorporated into the polymer. In one embodiment, the modifier becomes only in a secondary reactor given so that the radically polymerizable monomer in the primary reactor can polymerize.

condensation reactions between the modifiers and the condensation reactive functionalities The free radically polymerizable monomers are in general slow compared to free radical polymerization reactions. About that need out Condensation reactions generally high temperatures and long Reaction times to a satisfactory incorporation of the modifier to reach. Usually leads however an increase the reaction temperature to a reduction in the molecular weight of the polymers, which are formed by the free radical polymerization, and though due to a rise in the chain start rate and a rise the distribution of chain scission mechanisms. In typical radical polymerization reactions Thus, the temperature can rise to a point that the molecular weight of the obtained polymer product for its use is too low in the intended applications can. The incorporation of the multifunctional modifier in the polymer backbone increases however, the molecular weight of the polymer product through crosslinking, and may sufficient to decrease the molecular weight due to the temperature rise counteract.

In preferred method according to the invention are also one or more radically polymerizable monomers introduced into the reaction zone, which are virtually free of condensation-reactive functionalities. Examples for vinyl monomers include, but are not limited to, styrenic monomers, too known as vinyl aromatic monomers. Preferred vinylaromatic Monomers include α-methylstyrene and styrene. examples for other radically polymerizable monomers that are virtually free are of condensation reactive functionalities, include t-butylstyrene, o-chlorostyrene, Acrylonitrile and mixtures thereof.

In preferred method according to the invention are one or more radically polymerizable monomers with more than one vinyl group introduced into the reaction zone. These Divinyl monomers can optionally Contain condensation-reactive functionalities. Examples of such Monomers include divinylbenzene, 1,6-hexanediol diacrylate and ethylene glycol dimethacrylate. It is well known to those skilled in the art that to the extent that the temperature of the free radical polymerization increases, the molecular weight of the polymer formed decreases. However, they are often high temperatures necessary, to the desired Incorporation of the modifier in the polymer to achieve. The Use of divinyl species increases the molecular weight of the free Radical polymer and thus, in addition to the temperature, the residence time, the catalyst and the starter can be an important tool to achieve the goal of the Polymers, such as the molecular weight of the main chain and the Degree of installation to achieve modifier.

In contains preferred method the radically polymerizable monomer has a carboxyl functionality and the Modifier a hydroxy functional group. The reaction of the radically polymerizable monomer and the modifier thus leads to esterification with the release of water as a by-product. In more preferred method is acrylic acid as a radically polymerizable Monomer and cyclohexanol used as modifier. The Reaction of acrylic acid with cyclohexanol leads for the incorporation of cyclohexyl groups in the polymer product, resulting in a Coating product leads, the excellent weather resistance properties having. This weatherproof Coating may be noticeable after exposure to sunlight or UV light longer periods keep their shine. This becomes more specific in the following examples explained. Cyclohexyl acrylate can be purchased directly be acquired and by free radical polymerization in polymer products but the cost of cyclohexyl acrylate is prohibitive compared to the cost of acrylic acid and cyclohexanol. At the As described herein, the cyclohexyl group is unexpected high levels incorporated using cheap cyclohexanol and acrylic acid as a modifier and radically polymerizable monomer. Another preferred method comprises acrylic acid as a radically polymerizable Monomer and methylcyclohexylmethanol as modifier. In Another preferred method is butyl acrylate as radical polymerizable monomer and methylcyclohexylmethanol as monofunctional Modifier used. Methylcyclohexylmethanol estert with butyl acrylate to form an acrylate bond, the the methylcyclohexylmethyl group is incorporated into the polymer. At this Transesterification polymerization reaction uses butanol as a by-product educated.

It will be apparent to those skilled in the art that various combinations of radically polymerizable monomers containing condensation reactive functionalities, monofunctional modifiers, and radically polymerizable monomers that are virtually free of condensation reactive groups can be used in the desired proportions to form a polymer with the to obtain desired properties and characteristics. For example, common loadings of the primary polymerization reactor contain both styrene and α-methylstyrene in various proportions. Furthermore, combinations of acrylates and methacrylates can be used to tailor the composition and architecture of the product, as well as the final properties of the polymer, such as the glass transition temperature. The use of acrylates and methacrylates allows transesterification reactions with hydroxyl-containing modifiers. In one method of the invention, acrylic acid and styrene, α-methylstyrene, methyl methacrylate, butyl acrylate and cyclohexanol are added to the reactor together with a starter, a solvent and a catalyst 100 brought in. In this process, the monofunctional modifier cyclohexanol can react with the carboxyl group, and can also react with the ester groups on the butyl acrylate and methyl methacrylate to form a polymer product containing cyclohexyl acrylate and cyclohexyl methacrylate residues. The by-products of the reaction of cyclohexanol with butyl acrylate and methyl methacrylate are butanol and methanol, respectively. Thus, cyclohexyl groups can be incorporated into the polymer in a variety of ways.

In alternative methods are at least two different radical polymerizable monomers with one or more condensation reactive functionalities selected, to obtain a polymeric polymer having the desired properties. Usually For example, a mixture of these radically polymerizable monomers becomes continuous in the primary Polymerization reactor introduced. React in this process at least two different condensation reactive functionalities of the chosen radically polymerizable monomers with each other to either a diethylenically unsaturated Species or to create a crosslink between two polymer chains.

Although the polymerization and condensation process may be carried out without the use of a solvent, an inert solvent may optionally be introduced into the reaction zone of one of the reactors. Any suitable non-reactive solvent can be used in the process. Non-reactive or inert solvents are solvents that do not contain functionalities that react with the condensation-reactive functionality on the free-radically polymerizable monomer or with the functional group on the modifier. A reaction zone that is substantially free of inert solvent may contain as little as about 2 percent (w / w) of a reaction solvent, although the term normally designates a reaction zone containing less than that amount of solvent. Examples of suitable inert solvents include 1-methyl-2-pyrrolidinone, acetone, methyl amyl ketone, ^Isopar® G, a commercially available solvent from Exxon Chemicals (Houston, Texas), xylene, Aromatic 100 ^™ and Aromatic 150 ^™ , commercial aromatic solvents from Exxon Chemicals (Houston, Texas), hexane, heptane, toluene and diethylene glycol diethyl ether.

Although no catalysts are required in the polymerization and condensation process, various catalysts may preferably be used in the process. For example, in preferred processes, one or more catalysts capable of promoting a reaction between the condensation-reactive functionality of the monomer and the functional group of the modifying agent are preferably fed continuously into one of the reactors. Preferred catalysts include esterification catalysts, transesterification catalysts, and amidation catalysts. These include organic titanates, organic tin compounds, antimony oxides, organic sulfonic acids, mineral acids, metal acetates, Lewis acids and metal chlorides. Preferred catalysts include TYZOR ^® GBA, a titanate catalyst available from EI DuPont De Nemours & Co. (Wilmington, Delaware), dibutyl tin oxide, Sb ₂ O _3, p-toluenesulfonic acid, methanesulfonic acid, H ₂ SO _4, H ₃ PO _4, manganese acetate, Zinc acetate, dinonylnaphthalene disulfonic acid, hydrated monobutyltin oxide and zirconium oxide. Side reactions may occur under some conditions and undesirable by-products may form. The appropriate catalyst or group of catalysts should therefore be selected based on the reactants and reaction conditions.

Although not required for the polymerization and condensation process, various agents capable of reacting with a reaction by-product can be introduced into the reaction zone. Such agents are also referred to as by-product separation agents. Thus, the process may include one or more by-product separation agents capable of reacting with a condensation by-product being continuously introduced into one of the reactors. For example, cyclohexene reacts with water to form cyclohexanol, and may be added in amounts in the Reaction zone are introduced, which are effective to separate some or virtually all water by-product from a condensation reaction, such as an esterification reaction.

Even though not required, can be used in the polymerization and condensation process also a starter can be introduced into the reaction zone. Consequently The method preferably includes continuously feeding one or more radical polymerization initiator into a reactor. preferred Starters include peroxides such as di-t-butyl peroxide and di-t-amyl peroxide. Other suitable initiators include aliphatic Azo compounds such as 1-t-amylazo-1-cyancyclohexane, Azo-bis-isobutyronitrile and 1-t-butylazo-1-cyancyclohexane, and peroxides and Hydroperoxides such as t-butyl peroctoate, t-butyl perbenzoate, dicumyl peroxide, t-butyl hydroperoxide and cumene hydroperoxide.

Numerous continuous bulk polymerization processes are known in the art. Among them are U.S. Patent Nos. 4,414,370 issued to Hamielec et al .; 4,529,787 issued to Schmidt et al .; and 4,456,160 issued to Brand et al. With reference to the 1 and 2 An exemplary apparatus will now be described, wherein like numbers indicate like objects. The method comprises continuously introducing a mixture comprising at least one radically polymerizable monomer having a radically polymerizable group and also at least one condensation reactive functionality together with at least one modifier having a functional group capable of having the condensation reactive functionality on the radically polymerizable monomer to react in a primary reactor, such as the primary polymerization reactor 100 ( 1 ).

All modifiers in the reactor 100 are introduced in amounts which are effective to achieve sufficient incorporation of the modifier into the polymer product, and thus sufficient conversion of the reaction components into the polymer product. It may also contain more than one modifier in the reactor 100 are introduced so that a combination of modifiers is incorporated into the polymer product. In addition, one or more modifiers may be incorporated into a secondary reactor in the process. The continuous high temperature polymerization and condensation process comprises the step of heating the mixture in the primary polymerization reactor 100 to an effective temperature for a time sufficient to obtain a polymer product. At least a portion of the condensation reactive functionality reacts with the functional group of the modifier in the reaction zone such that at least a portion of the modifier is incorporated into the polymer product.

In addition, the effective temperature is maintained so that the polymer product is formed with virtually no gelation. The effective temperature is preferably between 175 ° C and 345 ° C. The average residence time is preferably less than 60 minutes in the primary reactor, and more preferably 2 to 60 minutes in the primary polymerization reactor 100 , Optionally, the primary reactor is vented. Exemplary primary reactors include a loop reactor and a stirred tank stirred tank reactor. Preferably, however, the primary reactor is a continuously stirred stirred tank reactor. The continuously stirred stirred tank reactor or the circulation reactor are equipped with stirring systems, so that the reactors are well mixed. The polymer product from the primary reactor 100 is continuously withdrawn from the reactor. The product can then be fed to another reactor or processed as the end product of the polymerization and condensation process.

continuous stirred stirred tank reactors and high reflux ratio cycle reactors have wide distributions the residence time, and therefore the extent to which the modifier in the primary Polymerization reactor is incorporated into the polymer product, heterogeneous be compared to a conventional one batch or semi-batch process. Thus, in unique polymer structures in this continuous process which were previously not available in the prior art.

In other alternative methods, the temperature of the primary reactor exceeds 100 300 ° C, and at least two radically polymerizable monomers, each having a radically polymerizable group and at least one condensation-reactive functionality, are fed to the reactor in the desired proportion. Optionally, a modifier can be added in the desired proportions to the reaction zone. Radically polymerizable monomers can react with each other to form a diethylenically unsaturated species and impart a high degree of crosslinking and / or branching to the polymer product. One of the reasons that gel formation is avoided is the high degree of chain termination by cleavage that occurs at the higher temperatures in the reaction zone. Thus, the polymer product has a high degree of branching. It is known that these polymers have improved rheological Show properties over linear polymers with comparable molecular mass, which were prepared in other ways.

In preferred processes, the mean residence time in the reaction zone of the primary reactor 100 kept in the range of 2 to 60 minutes. In the absence of a modifier, longer residence times will normally result in lower average molecular weights in the polymer product. This is a result of the increased conversion of the monomer (and initiator) species and the complex interaction of chain initiation kinetic rates, chain growth, and chain termination by cleavage. The addition of a suitable modifier could therefore reverse this trend, since condensation reactions are generally slower than free radical reactions, and their effect on molecular weight distribution is significantly enhanced by allowing longer residence times.

Generally introduces Temperature increase in reactions of this type to an increase in Degree of crosslinking for a given formula. The increased degree of crosslinking elevated usually the probability of gelation. unexpectedly However, the chain termination process that results from cleavage at higher temperatures results in counteracting this effect and thus delays the onset of the Gelling. Nevertheless, gel formation can occur in some formulations, when the temperature is over a certain limit is increased. However, the gelation behavior can be reversed if the Temperature further increased is then because the chain termination dominated and the molecular weight of the polymer product controlled. Gelation should therefore be avoided at every polymerization and condensation processes are considered.

at Methods that tend to gel differ in gelation behavior in a batch or semi-batch process from that in continuous reactors, because of the volatile nature the continuous process and because of the change in concentration free radicals and monomer species. Avoiding gelation is therefore much more difficult in batch reactors, and the process limits regarding composition and temperature are for the gel-free area much closer. If a polymerization and condensation process according to the present Invention in a continuous reactor at a temperature above the high temperature limit results in a highly branched, ungelled polymer structure.

As in the 1 and 2 In the continuous polymerization and condensation process, a secondary reactor can be used 200 be used. Optionally, but preferably, such a secondary reactor is vented. For example, a secondary reactor 200 in series with the primary polymerization reactor 100 be used. Exemplary secondary reactors include all reactors known in the art, such as, but not limited to, cycle reactors, tubular reactors, extruders and continuously stirred stirred tank reactors, or any other reactor suitable for continuous operation, including a combination of the above-mentioned reactors in series or in parallel. 1 shows as an exemplary secondary reactor 200 a tube reactor. The secondary tubular reactor 200 has one or more zones, such as the zones 202 and 204 , and can be equipped with static mixers. The zones 202 and 204 allow a variable, individual temperature control in each zone, and the zones 202 and 204 also provide individual, different Modifizierungsmittelzuleitungen 206 and 208 to disposal. The temperature in the secondary reactor is preferably maintained in the range of 175 ° C to 345 ° C, more preferably above 300 ° C, and the flow rates are adjusted so that the effective period in the secondary reactor is in the range of 2 to 300 minutes. In preferred polymerization and condensation processes, part of the modifier is through the leads 206 and 208 in the different zones 202 and 204 of the secondary reactor 200 brought in. The supply lines 206 and 208 also facilitate the supply of one or more catalysts, which in different proportions to the different zones 202 and 204 in the secondary tubular reactor 200 can be supplied. The additional secondary reactor 200 is used to increase overall residence time in the process, to increase the degree of incorporation of the modifier, and to increase the polymerization of the radically polymerizable monomers, both those having condensation reactive functionalities and those which are virtually free of such functionalities. Each tubular reactor used in the process preferably has one or more different polymerization reaction zones which allow for both individual temperature control and individual, different modifier streams. The catalysts are optionally supplied to different zones in the tube and they can be supplied in different proportions. In the process of the present invention, the secondary reactor 200 be arranged in different places. As in 1 For example, the secondary reactor may be between the primary reactor 100 and an evaporator known in the art, such as a conventional evaporator 106 , be arranged so that the polymer product from the primary reactor is fed into the secondary reactor, without passing through an evaporator is directed. As in 2 shown, the secondary reactor can 200 alternatively behind an evaporator, such as a conventional evaporator 106 to be ordered. Preferably, an evaporator, such as a conventional evaporator 106 , as in 1 shown behind the secondary reactor 200 arranged.

The conditions in the primary reactor 100 can be adjusted to achieve a desired product composition and molecular weight with relatively little incorporation of the modifier and the conditions of the secondary reactor 200 can be adjusted to increase the incorporation of the modifier. The modifier may be added to the feed mixture in the primary reactor 100 or optionally behind the primary reactor 100 in the inlet 206 of the secondary reactor 200 be introduced.

This variant of the method allows an architectural change in the structure of the polymer. The secondary reactor 200 is continuously mixed with the product mixture from the primary polymerization reactor 100 fed. The effective temperature is both in the primary polymerization reactor 100 as well as in the secondary reactor 200 controlled. The optimum effective temperature in each reactor 100 . 200 , is selected so that the desired product properties are obtained. Optionally, a catalyst in the secondary (polymerization) reactor 200 and the temperature at the reactors is adjusted so that the monomer sequence distribution in the polymer backbone can be changed to a desired distribution. The result of using this method and apparatus is that the molecular weight and architecture of the resulting polymer are tailored to a desired configuration and molecular weight.

In addition, a method of tailoring the architecture of the polymer chains is provided by adjusting the reaction conditions of the primary reactor 100 and the secondary reactor 200 to be changed. The supply of the modifier is in the primary reactor 100 , the secondary reactor 200 or both passed. A polymer product made from radically polymerizable monomers that tend to yield polymers with long sequences of a given monomeric unit (ie, polymers that are of a block-like nature) can be engineered to have a more random sequence length distribution with short sequences of each monomeric unit, starting from inexpensive precursors such as a radically polymerizable monomer and a modifier. This is possible because certain radically polymerizable monomers having condensation reactive functionalities, such as vinyl aromatic monomers, polymerize with other monomers in a more random manner than the monomer product obtained by the reaction between the radically polymerizable monomers and the modifier. Thus, polymers with a more random structure (I) can be selectively prepared where otherwise a polymer having a more block-like structure (II) would be obtained.

Examples for the Structure are shown above, where "A" is a radically polymerizable monomer with a condensation reactive Functionality, "B" a modifier and "C" a radically polymerizable monomer without representing a condensation-reactive functionality.

Furthermore For example, the polymer product of the present invention has a chain architecture and / or microstructure that is substantially different from that of a comparable one Polymer product, which only after a free radical polymerization was produced.

In continuous polymerization and condensation process, the gives a more random structure to a polymer product a precursor of a monomer that is traditionally long to form Sequences tends, along with other monomers in the primary reactor reacted to a polymer with a random distribution of monomeric To form units. In the secondary Polymerization reactor becomes the modifier by reaction with the condensation reactive groups on the precursor, which are in the polymer was polymerized, incorporated. Thus, polymers can be used in this process with short sequence length distributions the monomeric units prepared at the same total composition whereas, using conventional methods, only polymers are used with longer ones Sequence length distributions are possible.

In in the case where a specific acrylic acid derivative less easily with Styrene reacts as acrylic acid, would the Reaction between the acrylic acid derivative and styrene to long chain length sequences of the acrylate monomer in the polymer, whereas the reaction between acrylic acid and styrene in a more random distribution the chain length sequences would result. The latter reaction can be carried out after the continuous polymerization and condensation processes are carried out in the primary reactor, and the styrene / acrylic acid copolymer can then by reaction with the modifier in the primary reactor and / or the secondary reactor to the acrylate equivalent functionalized to produce the acrylate / styrene polymer, but with less long chain length sequences. As the entire modifier in the secondary reactor can be introduced, it is possible the formation of the Acrylsäureesterderivats in the primary Minimize polymerization. So if the modifier in the secondary reactor is introduced, the main part of the modifier reacts preferably with the condensation-reactive functionalities of in the primary reactor formed polymer product. It is sometimes preferable to the Incorporation of the modifier in the polymer in the second reactor of the process and to minimize in the primary reactor. In dependence from the choice of monomers, the choice of modifier and the reaction conditions, the method can also be used to produce a blocky polymer product while a more random Polymer normally be prepared by other methods would.

additional Reactors can in the continuous polymerization and condensation process be used in various places, such as, but not limited on intermediate devices after the primary and / or secondary reactor, such as an evaporator, the separation of volatile Materials, such as unreacted monomer, modifier and by-products from the polymer product. This extra Reactors can a cascade of continuously stirred boilers, circulation reactors, tubes, Extruders or plug flow reactors in different combinations, such as parallel or in series.

The process preferably comprises the substantial removal of unreacted monomer, reaction byproducts, the inert solvent, and optionally the unreacted modifier from the product mixture. This can be done using a conventional evaporator 106 be achieved, so that a polymer product is obtained, which is largely free of volatiles.

Reaction by-products, such as esterification water or transesterification methanol and various other side reactions, including starter decomposition products, may be present in the primary polymerization reactor 100 and in the secondary reactor 200 be formed. In addition, the reaction of the modifier with the condensation reactive functionality on the radically polymerizable monomer may be reversible. Thus, as known to those skilled in the art, the presence of by-products in the reactor can limit the conversion of the modifier. Therefore, the primary polymerization reactor 100 , the secondary reactor 200 or both preferably a vapor space 104 , Typical steam space reactors include continuously stirred stirred tank reactors. The liquid level in the reactor is generally kept constant by withdrawing the polymer product at the same mass rate as the feed is fed to the reactor. A vapor phase enriched in low boiling components is usually above the liquid level. Essential components of the vapor phase usually include low boiling by-products, solvents, unreacted monomers and unreacted modifier. In the case where reaction by-products are formed, the process preferably comprises continuous or periodic purging of the reaction by-products from the vapor space 104 of the primary polymerization reactor 100 to obtain a purge gas passing through the purge line 102 escapes. Preferably, the method also includes purging the vapor space in the secondary reactor 200 can be present. Preferably, an inert material, such as nitrogen, is used to purge the headspace of a reactor used in the continuous polymerization and condensation process to facilitate the separation of the by-products.

Unreacted monomer, reaction by-products, inert solvent, and unreacted, volatile modifier may be condensed and separated from the polymer product of the primary reactor or from the primary reactor itself. These materials can be in the capacitor 300 be condensed to obtain a liquid stream, which then enters the primary polymerization reactor 100 is introduced. Unreacted monomer, reaction by-products, inert solvent and unreacted modifier may also be separated from the polymer product of the secondary polymerization reactor or the secondary reactor by passing the material in the condenser 300 is condensed to obtain a liquid flow. This stream can then enter the primary polymerization reactor 100 or the secondary reactor 200 be introduced.

Preferably, unreacted monomer, reaction by-products, inert solvent and unreacted modifier will be from the primary polymerization reactor 100 or the secondary polymerization reactor 200 partially separated to obtain at least two streams, for example by partial condensation, distillation, membrane separation or centrifugation. More preferably, one of the streams is relatively free of reaction by-products. The stream, which is relatively free of reaction by-products, may be recycled to the primary polymerization reactor or optionally passed to the secondary polymerization reactor. In addition, the headspace purge gas from the primary or secondary reactor can be reacted with unreacted monomer, reaction byproducts, inert solvent and optionally unreacted modifier from the evaporator 106 be mixed and together in the condenser 300 be condensed.

Various Products can using the polymer product of the continuous polymerization and condensation method can be used. Some of them include Overprint varnishes, coatings, weather-resistant coatings, coating modifiers and mediators, dispersants, polymeric surfactants and polymers for colors.

The following non-limiting Examples are included to further the present invention to explain.

Examples

In the examples, the following abbreviations are used: 1,10-DD 1,10-decanediol 1,6-HD 1,6-hexanediol 2-EHA 2-ethylhexyl acrylate 2-EHAOH 2-ethylhexanol AA acrylic acid AMS α-methylstyrene AT acid number BA butyl acrylate CHDA 1,4-cyclohexanedicarboxylic acid CHOH cyclohexanol CSTR Continuously stirred stirred tank reactor DEGMEE diethylene DEGMEEA Diethylenglycolmonoethyletheracrylat DTBP Di-t-butyl peroxide EDA ethylenediamine EC ethylene glycol HEMA hydroxyethyl methacrylate IPA isophthalic IPDA Isofurondiamin MAK methyl amyl ketone MCHM 4-methylcyclohexyl methanol MMA methyl methacrylate M _n Number average molecular weight M _w Weight average molecular weight M _z z-average molecular weight NMP N-methylpyrrolidinone NV non-volatile shares PD Polydispersity index = (M _w / M _n ) PE polyester TBHP t-butyl hydroperoxide T _g Glass transition temperature TMP trimethylolpropane p-TSA p-toluenesulfonic acid

General procedure of polymer characterization

The in the examples described materials and products characterized by a number of standard techniques. The molecular weight Polymer products were purified by permeation chromatography ("GPC") techniques Use of tetrahydrofuran ("THF") as eluent and Polystyrene standards determined. The polystyrene standards used are currently available from Polymer Laboratories Limited (Church Streton, United Kingdom) and characterized by being number average molecular weights from 2250000, 1030000, 570000, 156000, 66000, 28500, 9200, 3250 and Have 1250. The hydroxyl numbers were determined by reaction with acetic anhydride solution and subsequent titration with standard base. Acid numbers were determined by titration determined with standard base. acid numbers are defined as the number of milligrams of potassium hydroxide needed to neutralize one gram of polymer. The hydroxyl numbers are defined as the number of milliequivalents of potassium hydroxide needed to neutralize one gram of polymer.

feed mixtures and unconverted volatile, Organic compounds were by gas chromatography (GC) under Using a Hewlett Packard DB-1 column measured. In some experiments was the concentration of carboxyl-containing monomers or modifiers determined by titration with standard base.

Continuous high-temperature polymerization, modified by condensation with a monofunctional modifier

example 1

A reaction mixture of 5% styrene, 17.5% acrylic acid, 15% 2-ethylhexyl acrylate, 32.45% methyl methacrylate, 30% cyclohexanol and 0.05% di-tert-butyl peroxide was continuously fed to a reactor process similar to that described in US Pat 1 which comprised a 11.36 L (3 gallon) CSTR followed by a fixed volume tube reaction zone, each zone maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to achieve a residence time of 15 minutes in the primary reactor. The residence time in the tube reactor zone was 30 minutes. The temperature of the primary reactor was maintained at 204 ° C while the temperature of the tube reaction zone was maintained at either 204 ° C, 232 ° C or 246 ° C. The reaction product was continuously pumped to a devolatilization zone and the polymer product from the devolatilization zone was collected continuously and later analyzed for the average molecular weights (M _w and M _n ) and acid number which determined the functionalized content Indicates carboxyl groups present on the polymer chains. The results of these reactions are shown in Table 1.

Table 1

Example 2

The procedure of Example 1 was repeated except that the reaction zone fill and feed flow rate were adjusted to achieve a 30 minute residence time in the primary reactor. The resulting residence time in the tube reactor zone was 30 minutes. The temperature of the primary reactor was maintained at 204 ° C while the temperature of the tube reaction zone was maintained at either 204 ° C or 232 ° C. The reaction product was continuously pumped to a devolatilization zone and the polymer product from the devolatilization zone was collected continuously and later for average molecular weights (M _w and M _n ) and acid number ana lysed, which indicates the content of functional groups present on the polymer chains. The results are shown in Table 2.

Table 2

Example 3

A reaction mixture of 5% styrene, 17.5% acrylic acid, 15% 2-ethylhexyl acrylate, 32.45% methyl methacrylate, about 30% cyclohexanol (see Table 3), 0.05% di-tert-butyl peroxide and various amounts of the esterification catalyst ( p-toluenesulfonic acid) was continuously fed to a reactor process similar to that described in US Pat 1 described that included only a 11.36 liter CSTR maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to provide a residence time of 15 minutes in the reaction zone. The temperature of the reaction zone was maintained at 204 ° C. Three different levels of p-toluenesulfonic acid were added to the reaction mixture, each in amounts representing 0.0%, 0.1% and 0.2% (by weight, respectively) of the reaction mixture. The reaction product was continuously pumped to a volatiles evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content indicates functional carboxyl groups present on the polymer chains. The results of these reactions are shown in Table 3.

Table 3

Example 4

A reaction mixture of 7.5% styrene, 15% acrylic acid, 17.5% butyl acrylate, 9.95% methyl methacrylate, 50% cyclohexanol, and 0.05% di-tert-butyl peroxide was continuously fed to a reactor process similar to that described in US Pat 1 which contained a 11.36 L CSTR followed by a fixed volume tube reaction zone, and each zone was maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to provide a 15 minute residence time in the CSTR. When used, the resulting residence time in the tube reaction zone was 18.75 minutes. The temperature of the CSTR was maintained at either 220 ° C or 245 ° C. The temperature of the tube reaction zone was maintained at 230 ° C when used. The reaction product was continuously pumped to a volatiles evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for the average molecular weights (M _w and M _n ) and acid number, which was the content indicates functional groups present on the polymer chains. The results of these reactions are shown in Table 4.

Table 4

Example 5

A reaction mixture of 10.5% styrene, 21% acrylic acid, 24.50% butyl acrylate, 13.95% methyl methacrylate, 30% cyclohexanol, and 0.05% di-tert-butyl peroxide was continuously fed to a reactor process similar to that described in US Pat 1 which contained a 11.36 L CSTR followed by a fixed volume tube reaction zone, and each zone was maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to provide a 15 minute residence time in the CSTR. When used, the resulting residence time in the tube reaction zone was 18.75 minutes. The temperature of the CSTR was maintained at 245 ° C. The temperature of the tube reaction zone was maintained at 230 ° C when used. The reaction product was continuously pumped to a volatiles evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for the average molecular weights (M _w and M _n ) and acid number, which was the content indicates functional carboxyl groups present on the polymer chains. The results of these reactions are shown in Table 5.

Table 5

Example 6

The procedure of Example 3 was repeated except that the reaction zone fill and feed flow rate were adjusted to achieve a 15 minute residence time in the reaction zone and that the temperature of the reaction zone was maintained at 232 ° C. Two different levels of p-toluenesulfonic acid were each added in amounts to the reaction mixture which were 0.1% and 0.2% (by weight) of the reaction mixture, respectively. The reaction product was continuously pumped to a volatiles evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for the average molecular weights (M _w and M _n ) and acid number, which was the content indicates functional carboxyl groups present on the polymer chains. The results of this reaction are shown in Table 6.

Table 6

Example 7

The procedure of Example 6 was repeated except that no p-toluenesulfonic acid was added to the reaction mixture and the temperature of the reaction zone was maintained at 246 ° C. The reaction product was continuously pumped to a volatiles evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content indicates functional carboxyl groups present on the polymer chains. The polymer product had a M _n of 1561, a M _w of 2780, and an acid number of 144.

Example 8

A reaction mixture of 14.39% styrene, 14.39% hydroxyethyl methacrylate, 28.52% butyl acrylate, 21.45% 4-methylcyclohexylmethanol, 21% methyl amyl ketone and 0.25% di-t-butyl peroxide was continuously added to a 500 ml CSTR which was maintained at a constant temperature of 232 ° C or 249 ° C. The feed flow rate was adjusted to achieve a residence time of 12 minutes. The reaction product was continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and polydispersity (PD). The volatile organic compounds were analyzed by gas chromatography. The amount of 4-methylcyclohexylmethanol incorporated into the polymer by transesterification was calculated by mass balance of the process and shown as a conversion. The results are shown in Table 7.

Table 7

The above experiment was repeated at 232 ° C with the same composition, except that the methyl amyl ketone is reduced to 20%, and 1% of a transesterification catalyst, tetraisopropoxy titanate (Tyzor ^® TPT, available from EI DuPont De Nemours & Co. (Wilmington, Delaware) ) was added to the monomer mixture. The results are shown in Table 8. This example demonstrates that extension of the polymer chain is obtained by reaction of the side hydroxyethyl groups with the butyl or hydroxyethyl ester of an adjacent polymer chain, resulting in the formation of crosslinks. This example also demonstrates that the use of an esterification catalyst increases the incorporation of alcohol into the polymer by transesterification

Table 8

Example 9

A reaction mixture of 29.78% styrene, 28.52% butyl acrylate, 21.45% 4-methylcyclohexanemethanol, 20% methyl amyl ketone and 0.25% di-t-butyl peroxide was passed continuously through a 500 ml CSTR operating at a constant pressure Temperature of 232 ° C or 249 ° C was maintained. The feed flow rate was adjusted to achieve a residence time of 12 minutes. The reaction product was continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and polydispersity (PD). The volatile organic compounds were analyzed by gas chromatography. The amount of 4-methylcyclohexanemethanol incorporated into the polymer by transesterification was calculated by a mass balance of the process and presented as a conversion. The above experiments were repeated with the same composition, except that the content of methyl amyl ketone to 20% reduced, and that 1% of a transesterification catalyst: tetraisopropoxy titanate (Tyzor ^® TPT) was added to the monomer mixture. The results are shown in Table 9.

Table 9

Example 10

A reaction mixture of 9.2% styrene, 9% 2-ethylhexyl acrylate, 15.2% acrylic acid, 33.85% methyl methacrylate (33.60% when 0.25% p-TSA was used), 31.5% 4- Methylcyclohexylmethanol and 0.25% di-t-butyl peroxide were passed continuously through a 500 ml CSTR maintained at a constant temperature of 193 ° C or 204 ° C. Another variable in this experiment was the addition of 0.25% p-toluenesulfonic acid based on total feed weight. The reaction zone fill level and feed flow rate were adjusted to achieve a 12 minute residence time. The reaction product was continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content of carboxyl functional groups present on the polymer chains. The analysis shows the formation of a medium molecular weight polymer having molecular weights and acid functionality which vary depending on the presence of a catalyst and the temperature of the reaction zone. The results are shown in Table 10.

Table 10

Example 11

A reaction mixture of 11% isobutyl acrylate, 20.5% acrylic acid, 26.5% methyl methacrylate (26.25% when 0.25% p-TSA was used), 41.55% 4-methylcyclohexylmethanol and 0.45% di- t-butyl peroxide was passed continuously through a 500 ml CSTR maintained at a constant temperature of 193 ° C or 204 ° C. Another variable in this experiment was the addition of 0.25% p-toluenesulfonic acid based on total feed weight. The reaction zone fill level and feed flow rate were adjusted to achieve a 12 minute residence time. The reaction product was continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content of carboxyl functional groups present on the polymer chains. The analysis shows the formation of a medium molecular weight polymer having molecular weights and acid functionality which vary depending on the presence of a catalyst and the temperature of the reaction zone. The results are shown in Table 11. The conversion to the ester is significantly higher when p-TSA is present.

Table 11

Example 12

A feed mixture of 9.2% styrene, 9% 2-ethylhexyl acrylate, 15.2% acrylic acid, 33.85% methyl methacrylate, 31.5% 4-methylcyclohexylmethanol and 0.25% di-t-butyl peroxide was continuously fed to a reactor process, similar to the one in 1 which contained a 11.63 L CSTR followed by a tube reaction zone, and each zone was maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to provide a 12 minute residence time in the CSTR. The resulting residence time in the tube reactor was 20 minutes. The temperature in the CSTR was maintained at 199 ° C and the temperature in the tube reactor was maintained at either 218 ° C or 246 ° C. The reaction product was continuously pumped to a volatilization evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content indicates functional carboxyl groups present on the polymer chain. The analysis shows that the acid functionality depends on the temperature of the tubular reactor. The results are shown in Table 12. The higher tube temperature significantly lowered the acid number, indicating a higher level of ester formation.

Table 12

Example 13

A feed mixture of 11% butyl acrylate, 20.5% acrylic acid, 26.5% methyl methacrylate, 41.55% 4-methylcyclohexylmethanol, and 0.45% di-t-butyl peroxide was continuously charged to a reactor process similar to that described in US Pat 1 introduced, which included a 11.63 l CSTR and behind a tubular reactor. The temperature of each reactor was maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to provide a 12 minute residence time in the CSTR. The resulting residence time in the tube reactor was 20 minutes. The temperature in the CSTR was maintained at 204 ° C and the temperature in the tube reactor was maintained at either 218 ° C or 246 ° C. The reaction product was continuously pumped to a volatilization evaporation zone, and the volatile product evaporation zone polymer product was continuously collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content indicates functional carboxyl groups present on the polymer chains. The analysis shows that the acid functionality depends on the temperature of the tubular reactor. The results are shown in Table 13. The higher tube temperature significantly lowers the acid number, indicating a higher level of ester formation.

Table 13

Example 14

This example demonstrates the utility of the process of this invention by demonstrating the difficulty in post-modifying resins with a modifier. A comparison with Example 1 shows a much lower incorporation of the modifier in batch experiments in an ampule compared to that achieved with the method of Example 1. A number of blends of different formula compositions comprising an acrylic polymer, a solvent, a monofunctional modifier, and an esterification catalyst were prepared. In each formula the acrylic polymer utilized was a styrene / α-methylstyrene / acrylic acid terpolymer having an acid number of 244 and a _Mn of 1130. Each formulation was prepared by dissolving 10 grams of the acrylic polymer in 23 grams of the solvent, followed by the addition a monofunctional modifier selected from the group consisting of cyclohexanol and 4-methylcyclohexylmethanol and the addition of an esterification catalyst selected from the group consisting of p-TSA, H ₃ PO ₄ , Mn (Ac) ₂ and Zn (Ac) ₂ . The amounts of monofunctional modifier and esterification catalyst used for each formulation are listed in Table 14. When the catalyst was p-TSA or H ₃ PO ₄ , the solvent used was MAK, while the solvent used was otherwise NMP.

Table 14

2 Grams of each formulation were each placed in two vials. These vials were after three freeze-thaw degassing cycles closed under vacuum. The ampoules were placed in an oil bath over a Period of 60 minutes to a constant temperature of 200 ° C heated. The ampoules were subsequently from the oil bath taken out, quenched and in terms of acid number, water content according to the Karl Fischer method and the residues by means of Gas chromatography analyzed. The results are in Table 15 listed. In some formulations, the formation of a cyclohexene by-product has been reported demonstrated.

Table 15

Example 15

A reaction mixture of 49% styrene, 21% acrylic acid, 30% NMP and 0.25% di-t-butyl peroxide is passed continuously through a 500 ml CSTR and maintained at a constant temperature of 232 ° C. The reaction zone fill level and feed flow rate are adjusted to achieve a 12 minute residence time. The reaction product is continuously stripped of volatile organic compounds, collected, and later analyzed for average molecular weights (M _w and M _n ) and acid number, which indicates the content of carboxyl functional groups present on the polymer chains.

Example 16

One Reaction mixture is prepared by adding 34% (by weight) Octylamine or cyclohexylamine to the monomer mixture of Example 15. The resulting mixture is passed through a 500 ml CSTR continuously passed on to either 218 ° C or 232 ° C is held.

The reaction zone fill level and feed flow rate are adjusted to achieve a 12 minute residence time. The reaction product is continuously devolatilized, collected, and later analyzed for average molecular weights (M _w and M _n ) and acid number, which indicates the level of unreacted carboxyl functional groups remaining on the polymer chains. It is noted that the molecular weight of the polymer increases as the side carboxyl groups react with the amine reagent.

Example 17

A reaction mixture of styrene, α-methylstyrene, acrylic acid, diethylene glycol monoethyl ether, xylene and di-tert-butyl peroxide (Table 16) were continuously subjected to a reactor process similar to that described in U.S. Pat 1 and containing a 11.63 L CSTR followed by a fixed volume tube reaction zone, and each zone was maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to provide a 12 minute residence time in the CSTR. The resulting residence time in the tube reaction zone was 15 minutes. The temperature of the CSTR was maintained at 193 ° C, 199 ° C or 204 ° C. The temperature of the tubular reactor was maintained at 260 ° C. The reaction product was continuously pumped to a volatile volatilization zone and the volatile product evaporation zone polymer product was continuously collected and later analyzed for average molecular weights (M _w and M _m ) and acid number indicating the content indicates functional carboxyl groups present on the polymer chains. The weight percentages of diethylene glycol monoethyl ether acrylate were calculated by a mass balance of the method. The results of these reactions are shown in Table 17.

Table 16

Table 17

Example 18

A reaction mixture is prepared by adding various levels of Cardura ^® E, an organic epoxy compound available from Shell Oil (New York, New York) to the monomer mixture of Example 15. The resulting mixture is continuously passed through a stirred 500 ml reaction zone to 218 ° C is maintained. The reaction zone fill level and feed flow rate are adjusted to achieve a 12 minute residence time. The reaction product is collected continuously and later visibly analyzed the average molecular weights (M _w and M _n ) and the acid number, which indicates the level of unreacted carboxyl functional groups remaining on the polymer chains. The analysis shows that increases in proportion as the content of Cardura ^® E in the formulation, an increase in molecular weight is observed and is accompanied by a decrease in acid number. This indicates that the reaction of the side carboxyl groups with the epoxy reagent yields a grafted polymer chain, resulting in the formation of graft polymers.

Continuous high-temperature polymerization, modified by condensation with a multifunctional, non-polymeric

modifiers

Example 19

A reaction mixture of 28% styrene, 34% acrylic acid and 38% α-methylstyrene monomers was passed continuously through a 400 ml CSTR maintained at a constant temperature. The feed flow rate was adjusted to achieve a residence time of 12 minutes. In this experiment no inert solvent or starter was used. The reaction product was collected continuously and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content of functional groups present on the polymer chains. The analysis shows the formation of a polymer of average molecular weight and molecular weights and acid functionality, which depend on the temperature of the reaction zone. The results are shown in Table 18.

Table 18

Example 20

A feed mixture was prepared by mixing styrene, α-methylstyrene, acrylic acid and ethylene glycol according to the compositions shown in Table 19. The resulting mixture was passed continuously through a 400 ml CSTR maintained at 271 ° C. The feed flow rate was adjusted to achieve a residence time of 12 minutes. In this experiment, no inert solvent or peroxide starter was used. The reaction product was collected continuously and analyzed later for average molecular weights (M _w and M _n ) and acid number indicating the level of unreacted carboxyl functional groups remaining on the polymer chains. The analysis shows that as the content of ethylene glycol in the formulation is increased, an increase in molecular weight is observed, accompanied by a decrease in the acid value. This shows that polymer chain extension is obtained by reaction of the side carboxyl groups with the glycol reagent, resulting in the formation of crosslinks. A slight broadening of the molecular weight distributions is observed, which is shown by the polydispersity index. The results are shown in Table 19.

Table 19

Example 21

The reaction mixtures of styrene, α-methylstyrene, acrylic acid and ethylene glycol shown in Table 20 were continuously passed through a 400 ml CSTR maintained at a constant temperature of 282 ° C. The feed flow rate was adjusted to achieve a residence time of 12 minutes. In this experiment, no inert solvent or peroxide starter was used. The reaction product was continuously stripped of volatile organic compounds, collected, and later analyzed for average molecular weights (M _w and M _n ), polydispersity (PD), and acid number, indicating the level of functional groups present on the polymer chains. The results are shown in Table 20.

Table 20

Example 21

The reaction mixtures of styrene, α-methylstyrene, acrylic acid and ethylene glycol described in Table 21 were continuously passed through a 400 ml CSTR maintained at a constant temperature of either 293 ° C or 296 ° C. The feed flow rate was adjusted to achieve a residence time of 12 minutes. In this experiment, no inert solvent or peroxide starter was used. The reaction product was continuously stripped of volatile organic compounds, collected, and later analyzed for average molecular weights (M _w and M _n ), polydispersity (PD), and acid number, indicating the level of carboxyl functional groups present on the polymer chains. The results are shown in Table 21. The analysis shows that as the ethylene glycol content in the formulation is increased, an increase in molecular weight is observed, accompanied by a decrease in acid number. This demonstrates that the reaction of the side carboxylic acid groups with the glycol reagent provides a polymer chain extension which results in the formation of crosslinks. A broadening of the molecular weight distribution is observed, which is shown by the polydispersity index. It has been observed that the use of an ethylene glycol content greater than 8% (w / w) occurs at the reaction zone temperature used in this example in the reactor as evidenced by the large increase in PD in the last run of Table 21.

Table 21

Example 23

The reaction mixtures of styrene, α-methylstyrene, acrylic acid and ethylene glycol shown in Table 22 were continuously passed through a 400 ml CSTR maintained at a constant temperature of 314 ° C. The feed flow rate was adjusted to achieve a residence time of 12 minutes. In this experiment, no inert solvent or peroxide starter was used. The reaction product was continuously separated from the reactor, collected, and later analyzed for average molecular weights (M _w and M _n ), polydispersity (PD), and acid number, indicating the content of carboxyl functional groups present on the polymer chains. The results are shown in Table 22. Analysis showed an increase in molecular weight accompanied by a decrease in acid number over a comparable polymer product made in the absence of ethylene glycol. This demonstrates that polymer chain extension is obtained from the reaction of the side carboxyl groups with the glycol reagent, resulting in the formation of crosslinks. Since no gel was observed, a comparison of the formulations of Example 22 illustrates the effect of chain termination by cleavage, suggesting the use of higher levels of EC possible when the temperature is increased.

Table 22

Example 24

A reaction feed mixture of 28.19% styrene, 37.42% α-methylstyrene, 33.39% acrylic acid and 1% ethylene glycol was passed continuously through a 400 ml CSTR maintained at a constant temperature of 282 ° C. The feed flow rate was adjusted to achieve a residence time of 30 minutes. In this experiment, no inert solvent or peroxide starter was used. The reaction product was continuously separated from the reactor, collected and later analyzed for average molecular weights (M _w and M _n ), polydispersity (PD) and acid number, indicating the content of carboxylic acid functional groups present on the polymer chains. The polymer product had an M _n of 870, an M _w of 1533, a PD of 1.76, and an acid number of 211.

Example 25

Reaction feed mixtures of styrene and acrylic acid monomers, xylene solvent, di-t-butyl peroxide initiator, and ethylene glycol modifier were prepared according to the formulations listed in Table 23. Each feed mixture was passed continuously through a 500 ml CSTR maintained at 249 ° C. The reaction zone fill level and feed flow rate were adjusted to achieve a 12 minute residence time. The reaction products were continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content of unreacted carboxyl functional groups remaining on the polymer chains. The analysis shows that as the multifunctional alcohol content in the formulation is increased, an increase in molecular weight is observed, accompanied by a decrease in acid number. This demonstrates that polymer chain extension is obtained from the reaction of the side carboxyl groups with the multifunctional alcohol reagents, resulting in the formation of crosslinks. A broadening of the molecular weight distributions is observed, which is shown by the polydispersity index. The results are shown in Table 24.

Table 23

Table 24

Example 26

Reaction feed mixtures of styrene, acrylic acid and 2-ethylhexyl acrylate monomers, xylene solvents, di-t-butyl peroxide initiators and a modifier (ethylene glycol (EG), 1,6-hexanediol (1,6-HD) or 1,10- Decanediol (1,10-DD)) were prepared according to the formulations listed in Table 25. Each feed mixture was passed continuously through a 500 ml CSTR maintained at 249 ° C. The reaction zone fill level and feed flow rate were adjusted to achieve a 12 minute residence time. The reaction products were continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content of unreacted carboxylic acid functional groups remaining on the polymer chains. The analysis shows that as the multifunctional alcohol content in the formulation is increased, an increase in molecular weight is observed, accompanied by a decrease in acid number. This demonstrates that polymer chain extension is obtained from the reaction of the side carboxyl groups with the multifunctional alcohol reagents, resulting in the formation of crosslinks. Broadening of molecular weight distributions is observed, as shown by the polydispersity index. The results are shown in Table 26.

Table 25

Table 26

Example 27

A reaction mixture of 42% styrene, 21% acrylic acid, 3.4% Dytek ^® A (a commercial product of DuPont, Wilmington, Delaware) 33.1% NMP and 0.5% DTBP is continuously passed through a 500 mL CSTR which is kept at 247 ° C. The reaction zone fill level and feed flow rate are adjusted to achieve a 12 minute residence time. A reaction product is obtained and analyzed for acid number, M _w and M _n .

Example 28

A reaction mixture of 42% styrene, 21% acrylic acid, 5.0% isofurondiamine, 31.5% NMP and 0.5% DTBP is passed continuously through a 500 ml CSTR maintained at 247 ° C. The reaction zone fill level and feed flow rate are adjusted to achieve a 12 minute residence time. A product is obtained and analyzed for acid number, M _w and M _n .

Table 27

Example 29

One Reaction mixture is prepared by adding various levels of either pentaerythritol or trimethylolpropane to the monomer mixture from Example 28. However, in the case of trimethylolpropane, it has been reported solvent Used xylene. The formulations are shown in Table 28.

Table 28

The resulting mixtures were passed continuously through a 500 ml CSTR maintained at 249 ° C. The reaction zone fill level and feed flow rate were adjusted to achieve a 12 minute residence time. The reaction products were continuously stripped of volatile organic compounds, collected and later analyzed for average molecular weights (M _w and M _n ) and acid number, indicating the content of unreacted carboxyl functional groups remaining on the polymer chains. The analysis shows that as the multifunctional alcohol content in the formulation is increased, an increase in molecular weight is observed, accompanied by a decrease in acid number. This demonstrates that polymer chain extension is obtained from the reaction of the side carboxyl groups with the multifunctional alcohol reagents, resulting in the formation of crosslinks. A slight broadening of the molecular weight distributions is observed, as shown by the polydispersity index. The results are shown in Table 29. Trimethylolpropane reacted less with respect to AN but M _w increased and broadened more than the pentaerythritol-containing examples.

Table 29

Example 30

A Number of mixtures of different formula compositions of acrylic acid, styrene, Caprolactam, di-t-butyl peroxide, xylene and p-TSA were prepared. The formulations are listed in Table 30. All ingredients were in the solvent and mixed for 20 minutes. 2 grams of each formulation were given in each case four ampoules. These ampoules were after closed three freeze-thaw degassing cycles under vacuum. One vial of each formulation listed in Table 30 was used in an oil bath heated at a constant temperature of 218 ° C over a period of 20 minutes. So did another set of ampoules in an oil bath 120 Heated for a few minutes. The procedure was over 20 minutes and 120 minutes at 246 ° C repeated. Subsequently the ampoules were removed from the oil bath taken out, quenched and in terms of molecular weight by means of GPC and the residual contents by gas chromatography analyzed. The reaction conditions are listed in Table 31.

Table 30

Table 31

Example 31

A reaction mixture of styrene, hydroxyethyl methacrylate (HEMA), adipic acid, 1-methyl-2-pyrrolidinone and di-tert-butyl peroxide (Table 32) was passed continuously through a 500 ml CSTR maintained at a constant temperature of 249 ° C , The feed flow rate was adjusted to achieve a residence time of 12 minutes. The reaction product was collected continuously from the reactor outlet but was not freed from volatile organic compounds. The product was later analyzed for the average molecular weights (M _w and M _n ) and polydispersity (PD), as well as the acid number, which indicates the content of hydroxy functional groups present on the polymer chains. The results of these reactions are shown in Table 33.

Table 32

Table 33

Example 32

A reaction mixture of styrene, 2-ethylhexyl acrylate, acrylic acid, methyl methacrylate, 4-methylcyclohexanemethanol, cyclohexanedimethanol and di-tert-butyl peroxide (Table 34) was passed continuously through a 500 ml CSTR operating at a constant temperature of either 232 ° C or 249 ° C was held. The reaction product was continuously stripped of volatile organic compounds, collected, and later analyzed for average molecular weights (M _w and M _n ), polydispersity (PD), and acid number, indicating the level of carboxyl functional groups present on the polymer chains. The results of these reactions are shown in Table 35. This example demonstrates that in the process both a monofunctional and a non-polymeric multifunctional modifier can be used simultaneously.

Table 34

Table 35

Continuous high-temperature polymerization, modified by condensation with a polymeric modifier

Example 33

A monomer mixture was prepared by mixing monomers in a weight ratio of 28.4 parts styrene, 33.8 parts acrylic acid and 37.8 parts α-methylstyrene monomer. A reaction mixture of the monomer mixture and different weight percent of Dow P425 ^™ , a polymeric polypropylene glycol modifier, available from The Dow Chemical Company (Midland, MI) as listed in Table 36, was passed continuously through a 500 ml CSTR operating on a constant temperature was maintained. The polymeric polypropylene glycol modifier had an M _n of 425 and an average functionality of two hydroxyl-condensation reactive groups on each chain. The reaction zone fill level and feed flow rate were adjusted to provide a hold time of 12 or 24 minutes, as shown in Table 36. The temperature of the reaction zone was maintained at 282 ° C. The reaction product was collected continuously and analyzed later for average molecular weights (M _n , M _w and M _z ) and acid number indicating the content of carboxyl functional groups present on the polymer chains. The results are shown in Table 36.

Table 36

Example 34

The product of four different formulations (33b, 33d, 33e, and 33g) collected from the CSTR in Example 33 was placed in a 1000 ml reactor and subjected to a continuous heat treatment for a specified period of time at a constant temperature. The reaction product was again analyzed _for average molecular weights (M _n , M _w , M _z ) and acid number, indicating the content of carboxyl functional groups remaining on the polymer chains. The analytical results are shown in Table 37 along with the time and temperature used for each formulation. The analysis shows that the acid number of the polymer product had decreased after the heat treatment while its M _{w had increased} without formation of a gel product. This demonstrates the possibility of using a plug flow reaction zone as the secondary reactor behind the CSTR of Example 33 to increase the degree of condensation between the polymer product and the polymeric modifier.

Table 37

Example 35

Reaction feed mixtures of styrene, acrylic acid and α-methylstyrene monomers, di-t-butyl peroxide free radical initiator, methyl amyl ketone solvent and a polymeric modifier were prepared as shown in Table 38. The polymeric modifying agent was Rucote ^® 112, a polyester available from Ruco Polymer Corp. (Hicksville, New York), which had a M _n of 4233. Each of these mixtures was continuously passed through a 500 ml CSTR maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to achieve a 12 minute residence time. The temperature of the reaction zone was maintained at 204 ° C. The reaction product was collected continuously and analyzed later for average molecular weights (M _n , M _w and M _z ) and acid number, indicating the content of carboxyl functional groups present on the polymer chains. The polymer product properties are shown in Table 39.

Table 38

Table 39

Example 36

The reaction product collected from the CSTR in Example 35a was placed in a 1000 ml reactor and subjected to a continuous heat treatment at different time periods as shown in Table 40 at a constant temperature of 220 ° C. The reaction product was analyzed again for the average molecular weights (M _n , M _w and M _z ) and the acid number, indicating the content of carboxyl functional groups remaining on the polymer chains. The analysis shows that as the heat treatment period is increased, the acid number of the reaction product decreases and its molecular weight increases without formation of a gel product. This demonstrates the possibility of using a plug flow reaction zone as the secondary reactor behind the CSTR of Example 35a to increase the degree of condensation between the polymer product and the polymeric modifier. The results are shown in Table 40.

Table 40

Example 37

The reaction product collected from the CSTR in Example 35b was placed in a 1000 ml reactor and subjected to a continuous heat treatment at different time periods as shown in Table 41 at a constant temperature of 220 ° C. The reaction product was analyzed again for the average molecular weights (M _n , M _w and M _z ) and the acid number, indicating the content of carboxyl functional groups remaining on the polymer chains. The analysis shows that as the heat treatment period is increased, the acid number of the reaction product decreases and its molecular weight increases without formation of a gel product. This demonstrates the possibility of using a tube reaction zone as the secondary reactor behind the CSTR of Example 35b to increase the degree of condensation between the polymer product and the polymeric modifier. The results are shown in Table 41.

Table 41

Example 38

Reaction feed mixtures of styrene, acrylic acid, α-methylstyrene and 2-ethylhexyl acrylate monomers, di-t-butyl peroxide free radical initiator, methyl amyl ketone solvent and a polymeric modifier were prepared as listed in Table 42. The polymeric modifying agent was a polyester (Rucote ^® 112) having a M _n of 4233. Each of these mixtures was continuously passed through a 500 mL CSTR maintained at a constant temperature. The reaction zone fill level and feed flow rate were adjusted to achieve the residence time shown in Table 42. The temperature of the reaction zone was maintained at a constant temperature as shown in Table 42. The reaction product was collected continuously and analyzed later for the average molecular weights (M _n , M _w and M _z ) and the acid number indicating the content of carboxyl functional groups present on the polymer chains. The properties of the polymer product from the evaporator outlet are shown in Table 43.

Table 42

Table 43

Example 39

This example describes the preparation of a linear polyester for use as a polymeric modifier in the examples below. This linear polyester was prepared from the formulation shown in Table 44. The MP-diol, isophthalic and Fascat ^® 4100, a hydrated monobutyltin oxide available from Elf Atochem (Paris, France) were placed in a reactor equipped with a packed column. The mixture was heated to 210 ° C for three hours while maintaining the temperature of the column at 97 ° C. About 6.5% by weight of water was collected. The reaction was cooled to 116 ° C and 1,4-cyclohexanedicarboxylic acid was added. The reaction was then heated to 216 ° C for two hours. Subsequently, the column was bypassed to allow the separation of water. The reaction temperature was raised to 229 ° C for an additional 1.5 hours, and 6.4% by weight of water was collected from this second stage of the reaction. The final polymer properties are shown in Table 45.

Table 44

Table 45

Example 40

Reaction feed mixtures of styrene, acrylic acid, α-methylstyrene and 2-ethylhexyl acrylate monomials Di-t-butyl peroxide free radical initiator, methyl amyl ketone solvent and a polymeric modifier were prepared as listed in Table 46. The polymeric modifier was the linear polyester prepared in Example 39. Each of these mixtures was continuously passed through a 500 ml CSTR maintained at a constant temperature. The reaction zone level and feed flow rate were adjusted to achieve the residence time shown in Table 46. The temperature of the reaction zone was maintained at a constant temperature as shown in Table 46. The reaction product was collected continuously and analyzed later for the average molecular weights (M _n , M _w and M _z ) and the acid number indicating the content of carboxyl functional groups present on the polymer chains. The properties of the polymer product from the evaporator outlet are shown in Table 47.

Table 46

Table 47

Example 41

The The procedure of Example 40 was repeated under the same conditions and with the same compositions as in the mixtures 40a, 40b, 40c and 40d repeated, except 0.2% by weight of the esterification catalyst p-toluenesulfonic acid instead of 0.2% by weight Methyl amyl ketone solvent were added to the feed mixture. The newly obtained feed mixtures are 41a, 41b, 41c and 41d. The results of the analysis of the polymer product are shown in Table 48.

Table 48

The Results show that the addition of the esterification catalyst p-TSA the degree of esterification of Reaction increased, which is due to the higher molecular weights and lower acid numbers the polymer products obtained in Example 41 compared to those from Example 40 shows.

Example 42

The reaction product obtained from the CSTR in Example 40b was placed in a 1000 ml reactor and subjected to a continuous heat treatment at a constant temperature of 240 ° C for various periods of time listed in Table 49. The reaction product was analyzed again for the average molecular weights (M _n , M _w and M _z ) and the acid number, indicating the content of carboxyl functional groups remaining on the polymer chains. The analysis shows that as the heat treatment period is increased, the acid number of the reaction product decreases and its molecular weight increases without formation of a gel product. This demonstrates the utility of using a plug flow reaction zone as the secondary reactor behind the CSTR of Example 40b to increase the degree of condensation between the polymer product and the polymeric modifier. The results are shown in Table 49.

Table 49

Example 43

The conditions of Example 40c were repeated. The reaction product was collected from the CSTR, placed in a 1000 ml reactor and subjected to continuous heat treatment for a period of time as shown in Table 50 at a constant temperature of 240 ° C. The reaction product was analyzed again for the average molecular weights (M _n , M _w and M _z ) and the acid number, indicating the content of carboxyl functional groups remaining on the polymer chains. The analysis shows that as the heat treatment time is increased, the acid number of the reaction product decreases and its molecular weight increases, without formation of a gel product, up to a reaction time of 45 minutes. This demonstrates the utility of using a plug flow reaction zone with a suitably selected residence time as the secondary reactor behind the CSTR of Example 40c to increase the degree of condensation between the polymer product and the polymeric modifier. The results are shown in Table 50. As shown, gelation had occurred in the polymer product collected after 90 minutes, suggesting that the residence time suitable for operation must be kept at a lower level.

Table 50

Example 44

One Feed mixture was prepared as listed in Table 51, and a CSTR supplied with a downstream tubular reactor. The Residence time of the CSTR was maintained at 15 minutes and 222 ° C. The Röhrenverweilzeit was 20 minutes at a temperature of 232 ° C. The resulting polymer was collected from the evaporator. The polyester of Example 39 is used in this example.

Table 51

Example 45

The Feed blends are prepared as listed in Table 52. The CSTR feed mixture is fed at 236 g / min (0.52 lbs / min) while the level in the CSTR is adjusted so that a residence time of 15 minutes is maintained while the temperature at 222 ° C is held. The effluent of the CSTR is fed to a tube reactor where he with the listed in Table 52 Tube feed mixture is united. The polyester feed into the tubes is at 127 g / min (0.28 lbs / min). The residence time in the tube reactor is 20 minutes, and the temperature is maintained at 232 ° C. The resulting polymer is collected from the evaporator.

Table 52

Example 46

The Feed mixture was prepared as listed in Table 53, and fed to a CSTR. The residence time of the CSTR was maintained at 271 ° C for 30 minutes. The resulting polymer was collected from the evaporator. The polyester from Example 39 is used in this example.

Table 53

Example 47

The Conditions of Example 40a are repeated except that the polyester is melted and fed to the reactor separately. The resulting polymer is collected from the evaporator.

Example 48

This example describes the preparation of a polyamide for use as a polymeric modifier in the examples below. This polyamide was prepared from the formulation shown in Table 54. Sylvadyme ^TM T18, a dimerized fatty acid available from Arizona Chemical Company (Panama City, Florida), Adogen ^® 140D, a hydrogenated tallow amine available from Witco Corp. (Dublin, Ohio) and ethylenediamine were placed in a reactor, heated to 104 ° C and held for one hour. The 2-methyl-1,5-diaminopentane was then added to the reactor over 5 minutes. The reaction was heated to 193 ° C for 5 hours. The amount of water collected from the reaction was 4.3% by weight. The final polymer properties are shown in Table 55.

Table 54

Table 55

Example 49

Reaction feed mixtures of styrene, acrylic acid, α-methylstyrene and 2-ethylhexyl acrylate monomers, di-t-butyl peroxide free radical initiator, NMP solvent and a polymeric modifier were prepared as shown in Table 56. The polymeric modifier was the polyamide prepared in Example 48. Each of these mixtures was continuously passed through a 500 ml CSTR maintained at a constant temperature. The reaction zone level and feed flow rate were adjusted to achieve the residence time shown in Table 56. The temperature of the reaction zone was maintained at a constant temperature as shown in Table 56. The reaction product was collected continuously and analyzed later for average molecular weights (M _n , M _w and M _z ) and acid number indicating the content of carboxyl functional groups present on the polymer chains. The properties of the polymer product from the evaporator outlet are shown in Table 57.

Table 56

Table 57

Example 50

The Conditions from Example 49e are repeated except that the polyamide is melted and fed to the reactor separately. The resulting polymer is collected from the evaporator.

Example 51

A surfactant solution was prepared by dissolving 461 grams of the polymer of Example 26d in 960 grams of deionized water and 91 grams of 28% ammonia over 150 minutes at 80 ° C. The resulting solution had the properties shown in Table 58.

Table 58

Example 52

An emulsion polymer was prepared using 430 grams of the surfactant solution of Example 51, 9.9 grams of 28% ammonia, 127 grams of deionized water, 3.6 grams of Dow P1200 ^™ , a propylene glycol available from The Dow Chemical Company (Midland, et al. MI), and 0.3 grams of Tergitol ^® 15-S-9, a mixture of ethoxylated secondary C11-C15 alcohols, available given by Union Carbide (Danbury, Connecticut), and in a glass reactor equipped with a stirrer and a temperature control was. The mixture was heated to 83 ° C and then 17.5 grams of a 15% ammonium persulfate solution in deionized water was added to the reactor. A mixture of 77.5 grams of 2-ethylhexyl acrylate, 180.9 grams of methyl methacrylate and 7.0 grams of Tergitol ^® 15-S-9 was introduced over 75 minutes into the reactor. An additional 112 grams of the surfactant from Example 51 were added to the reactor after 50 minutes in the monomer feed. 58 minutes into the monomer feed in 31 grams of 16% sodium BASF-Pluronic ^® F127, optionally a block copolymer of ethylene oxide and propylene oxide available from BASF (Ludwigshafen, Germany) in deionized water in the reactor. At the end of the addition, 0.9 grams of t-butyl hydroperoxide was added to the reactor. Subsequently, 1.64 grams of a 9% sodium erythorbate solution in deionized water was added to the reactor. The contents were held for 15 minutes and then cooled. The resulting emulsion polymer was relatively free of coagulation and had the properties listed in Table 59. This example demonstrates the utility of using the polymer of Example 26d as a surfactant stabilizer for an emulsion polymer.

Table 59

Example 53

One Color modifier was prepared using 204.2 Grams of the polymer of Example 49h, deionized in 337.6 grams Water and 8.2 grams of 28% ammonia was dissolved. The resulting solution was used as a coating modifier.

Example 54

A comparative coating was prepared as follows. Joncryl ^® -819, an acrylic polymer available from SC Johnson & Sons, Inc., (Racine, Wisconsin), (270 parts), 1.5 parts benzoin, 5.0 parts MODAF ^low® , a commercial product available from Monsanto Chemical Company (St. Louis, Missouri), 185.4 parts R-960 ^™ -TiO ₂ , a product of EI Du Pont De Nemours & Co. (Wilmington, Delaware) and U.S. Patent Nos. 4,846,074; 37.7 parts of triglycidyl isocyanurate were combined and mixed together. The formulation was mixed and sprayed by a standard powder coating method. The coated panel was heated at 190 ° C for 20 minutes to give a high-gloss 0.05 mm (2 mil) film.

A coating containing a polymer product of the present invention was prepared using the polymer product of Example 9b. The product of Example 9b is R-960 ^TM TiO ₂ and triglycidylisocyanurate is mixed with appropriate amounts of benzoin, Modaflow7. The formulation is mixed and sprayed on by a standard powder coating method. The coated panel is heated at 190 ° C for 20 minutes to give a high-gloss 0.05 mm (2 mil) film.

Example 55

The emulsion of Example 52 (47 parts), Joncryl ^® 52 resin (30 parts), Jonwax ^® 26, a wax emulsion product available from SC Johnson & Sons, Inc. (Racine, Wisconsin) (8.0 parts), ethylene glycol monobutyl ether ( 4.0 parts) and water (11 parts) are mixed together to prepare a coating varnish. The coating lacquer can be applied, for example, to paper or cardboard.

Example 56

One Feed mixture is prepared as in Table 60 and a CSTR fed. The residence time is maintained at 320 ° C for 15 minutes, and the resulting Polymer is collected from the evaporator.

Table 60

Claims (13)

Continuous polymerization and condensation process, this includes: (a) continuous introduction into a primary reactor from: (i) at least one free radically polymerizable monomer with a radically polymerizable group and also at least a condensation reactive functionality; and (ii) at least a modifier having a functional group that is in is capable of using the condensation-reactive functionality on the radical polymerizable monomer, wherein each modifier is a monohydric alcohol, and wherein any modifier does not have the formula ROH, in which R is a linear or branched one Alkyl radical having more than 11 carbon atoms; and (B) Maintaining an effective temperature in the primary reactor, to cause the polymerization of the monomer and at least to allow some of the condensation-reactive functionality to react with the functional group of the modifier, wherein a first polymer product is produced, the at least contains a part of the modifier. Continuous polymerization and condensation process according to claim 1, wherein the method further incorporating the first Polymer product from the primary reactor in a secondary reactor and further polymerizing the first polymer product to to produce a second polymer product, and the continuous one Withdrawing the second polymer product from the secondary reactor includes. Continuous polymerization and condensation process according to claim 2, further introducing the second polymer product in an extruder and the loading of the extruder reactor with an additional Modifier comprises to produce a third polymer product. Continuous polymerization and condensation process according to one of claims 2 or 3, where in the secondary reactor has at least two different reaction zones, wherein the temperature of each reaction zone is independently controlled. Continuous polymerization and condensation process according to one of the claims 1-4, wherein the Temperature in at least one reactor or a reactor zone between 175 ° C and 345 ° C is maintained. Continuous polymerization and condensation process according to one of the claims 1-5, that continues maintaining a flow rate through the primary reactor comprises a mean residence time of less than 60 minutes in the primary reactor to disposal to deliver. Continuous polymerization and condensation process according to one of the claims 1-6, that continues separating a volatile Materials from the primary reactor includes to two streams to receive, taking one of the streams contains unreacted starting materials and is relatively free of by-products. Continuous polymerization and condensation process according to one of the claims 1-7, wherein at least two different radically polymerizable monomers in the primary reactor be introduced. Continuous polymerization and condensation process according to one of the claims 1-8, in which the radically polymerizable monomer at least two different Has condensation-reactive functionalities. Continuous polymerization and condensation process according to one of the claims 1-9, in which the radically polymerizable monomers at least two vinyl groups to have. Continuous polymerization and condensation process according to one of the claims 1-10, wherein the condensation reactive functionality is selected from the group consisting of consists of a carboxyl, ester, anhydride, epoxy, amide and isocyanate functionality. Continuous polymerization and condensation process according to one of the claims 1-11, wherein the first polymer product is at least one cyclohexyl group includes. Lacquer coating, Coating, coating modifiers and leveling agents, dispersants, polymeric surface-active A composition or a paint comprising a polymer product, which the continuous polymerization and condensation process according to a the claims 1 to 12 is made.